WO2017142494A1 - Procédé de récupération à volume élevé d'eau de traitement et d'acquisition de produit économique à partir de lactosérum - Google Patents

Procédé de récupération à volume élevé d'eau de traitement et d'acquisition de produit économique à partir de lactosérum Download PDF

Info

Publication number
WO2017142494A1
WO2017142494A1 PCT/TR2016/050573 TR2016050573W WO2017142494A1 WO 2017142494 A1 WO2017142494 A1 WO 2017142494A1 TR 2016050573 W TR2016050573 W TR 2016050573W WO 2017142494 A1 WO2017142494 A1 WO 2017142494A1
Authority
WO
WIPO (PCT)
Prior art keywords
whey
water
membrane
draw solution
production
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/TR2016/050573
Other languages
English (en)
Inventor
Coskun AYDINER
Bulent Keskinler
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Gebze Teknik Universitesi
Original Assignee
Gebze Teknik Universitesi
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Gebze Teknik Universitesi filed Critical Gebze Teknik Universitesi
Publication of WO2017142494A1 publication Critical patent/WO2017142494A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; PREPARATION THEREOF
    • A23C1/00—Concentration, evaporation or drying
    • A23C1/12—Concentration by evaporation
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; PREPARATION THEREOF
    • A23C21/00—Whey; Whey preparations
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/002—Forward osmosis or direct osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/58—Multistep processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/445—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by forward osmosis
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; PREPARATION THEREOF
    • A23C2210/00—Physical treatment of dairy products
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; PREPARATION THEREOF
    • A23C2210/00—Physical treatment of dairy products
    • A23C2210/20—Treatment using membranes, including sterile filtration
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2002/00—Food compositions, function of food ingredients or processes for food or foodstuffs
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
    • C02F2103/327—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from processes relating to the production of dairy products
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • This invention is related to a method based on the use of innovative membrane systems with different combinations, which deals with whey as cheese production wastewater that should be significantly taken into account in relation to environmental pollution from the dairy industry; in comparison to pressure-driven membrane process combinations in common use (32-40% water recovery and production of concentrated whey in 15-20% solid content), whose main purpose is to both recover water from whey at higher water recovery percentages (65-80%) having reusable quality in the production process and to technically and commercially enable increased economic production of whey powder by means of concentrated whey obtainment having higher solid percentages (25-35%).
  • Milk and milk products industry includes plants in which milk is processed and converted into milk products such as raw milk, drinking milk, yoghurt and buttermilk, butter, cheese, ice cream, condensed milk, milk powder, baby food, and concentrated and dried whey.
  • Milk processing plants which are available in our country have various sizes and have complex structure as technologies and other characteristics.
  • the main source of pollutant of wastewaters originating from the dairy industry is the whey which is formed as a result of cheese production and has a lot of pollutant effects because of high nutrient content (C, N, P). Approximately 90 kg of the 100 kg milk which is processed for cheese emerges as whey. In this regard, in our country in 2002 considering that 564,000 ton milk is consumed to produce cheese, it is estimated that approximately 508,000 ton cheese whey is produced across the country.
  • Cheese whey contains 93-94% water, 4.5-6.0% lactose, 2.0-5.0% casein, 0.6-1.1% dissolved protein, 0.8-1.0%) mineral, 0.05-0.9%) lactic acid, 0.06-0.5%) fat as essential compounds.
  • Two types of whey exist, which are sweet (pH 6.5) and sour (pH ⁇ 5.0).
  • Average water quality has characteristics of 7.0-10.0 mS/cm conductivity, 800-1500 mg chloride/L, 60,000-90,000 mg COD/L, 900-1200 mg total nitrogen/L, 200-900 mg total phosphorus/L.
  • raw wastewater is concentrated by membrane processes in the first step, recovery of filtered effluent wastewater as demineralized water or process water and thereafter evaporating the water in concentrated whey stream so as to whey powder production.
  • whey powder can be concentrated conventionally by industrial methods such as direct or vacuum evaporation and spray drying, pre-concentration by membrane filtration prior to the main concentration process is especially preferred in the sense that whey powder in higher quality is gained from membrane concentrate streams; not only for decreasing energy cost and total plant operating cost in whey powder production, but also minimal protein decay effect at lower process temperatures ( ⁇ 60°C).
  • MF and UF processes are utilized in separating relative large molecular weighted whey proteins (caseins) and fats from smaller molecular weighted whey proteins (a- lactalbumin, ⁇ -lactoglobulin, etc.), lactose and minerals.
  • Production of whey protein concentrates by UF process is carried out in concentrations around 35% to 85%. However, for obtaining 70-85%) production levels, utilizing of MF prior to UF process is necessary for removing fat in raw whey.
  • proteins can be concentrated as well as for production of whey protein concentrates and isolates; lactose and salt can be removed simultaneously.
  • inclusion of divalent salts that have positive contribution to health is preferred for whey powder of good quality; for this purpose, production of whey powder having the targeted quality, can be carried out over NF concentrate stream by applying NF after UF.
  • Recovering water and producing concentrate whey stream by treating raw whey by means of pressure-driven processes, MF/NF, UF/NF, UF/RO, F/NF and F/RO combinations in the forms of industrial applications are effectively used; the UF/RO membrane system among these applications is mostly preferred because of easy operability in worldwide applications and economic viability.
  • a main concentrate stream is formed by collecting together concentrate streams of membrane processes in the whole system.
  • UF/RO 5% initial solid content of whey is increased to levels of 15-20% by means of UF process in the first step and thereafter recovered water is produced from UF permeate stream by single step or sequential two steps processing in RO process in the next step.
  • joint concentrate stream is produced by combining RO concentrate streams produced up to high concentrate ratios of >75% per process with UF concentrate stream; afterwards whey powder is produced by using the joint concentrate stream in which the concentrate is subjected to water removal using one of the processes such as direct evaporation, vacuum evaporation or spray drying.
  • the UF process which is applied in the first step is limited factor.
  • application pressure in UF has to be higher than the osmotic pressure of whey. This leads to a concentrate ratio in the UF process which is not as high as the ratio in RO.
  • diafiltration by diluting whey which is concentrated in UF in advance of RO, diluted UF whey stream is again filtrated in sequential two or more step UF processing prior to RO; increases in both the UF process step and membrane module number, not only makes it difficult for the simple operation of the system to be carried out, but it also it causes the investment and operation costs to increase and therefore it reduces the preferability of the application in practice.
  • diafiltration is mostly applied in UF/NF system integrity for the purpose of separation of protein and lactose; at this point, protein liquid is utilized generally in commercial beverage production.
  • Forward osmosis process is a membrane process depending on osmosis (movement of water from the low pressure side to the high pressure side through a semi permeable membrane due to osmotic pressure difference).
  • a semi-permeable membrane permits water while it prevents dissolved molecules or ions to pass through.
  • osmotic pressure of a liquid is proportional to dissolved matter concentration in definite volume solvent
  • effectiveness of water passage in an osmotic process depends on osmotic pressure difference between solutions at each side of the membrane without necessitating hydraulic or hydrostatic pressure.
  • FO process water transport can be provided even from wastewaters with high pollutant levels to the solution, having high osmotic pressure (draw solution) and whereby volume stream of wastewater feed can be decreased.
  • Fundamental advantages of the FO process are known as the low fouling tendency and the rejection (filtration) of pollutant matters at very high proportions and having much lower energy requirement and design costs compared to pressure-driven membrane processes.
  • utilization of FO becomes rather valuable especially in the food industry.
  • the main disadvantage of the process is the need of reconcentration of draw solution having high osmotic pressure. This disadvantage can be removed by water recovery based on combining FO draw solution with an external process (such as RO or MD).
  • the process can be utilized in various applications such as sea water desalination, wastewater treatment, drinking water production, clean water production from brackish water, food beverages or liquid food concentration (fruit juice and protein liquids) and alcohol dehydration.
  • MD process is a process in which the driving force of the process is temperature, micro porous membrane material is utilized and good quality of treated water is gained by high filtration performance (except for volatile organics, dissolved organics and inorganics 99% and above).
  • the passing of water through the membrane is provided during the vapour phase under heat difference without applying pressure, while the penetration of water stream in liquid feed stream into membrane pores is prevented.
  • Treated water is obtained by condensing water vapour passing through the membrane to the cold stream side.
  • the process can be applied having four different contents including direct contact, air gap, sweeping gas and vacuum.
  • the afore mentioned Combined RO applications of innovative membrane processes have effective field applicability potential in various areas ranging from clean water production to industrial wastewater treatment and industrial water recovery.
  • the RO process is a membrane process which possesses the lowest molecular size of separation among the pressure-driven membrane processes, and its process dynamics and field effectiveness are very well known nowadays.
  • very low molecular weighted dissolved organics (100 Da) as well as monovalent dissolved inorganics can be rejected at high filtration performance (99% and above) from the water environment.
  • the process can be used commonly in order to recover water from wastewater received from different industries and to produce process water and clean water with good quality for industrial usage primarily to produce drinking water from seawater.
  • EP 1046344 of the known state of the art, a method which uses membrane filtration and membrane ultrafiltration in order to obtain protein concentrate form whey is described.
  • the applications mentioned in these documents may sometimes be insufficient to reach the desired results.
  • the invention intends to carry out a method comprising basically two steps in terms of technology and three different steps in terms of membrane process content such as whey concentration, water recovery for reuse and obtaining whey powder, which aims to produce concentrated whey stream having high solid content by dehydration of whey which is obtained as a by-product following cheese production activities, during the first step membrane process using technological configurations having novel membrane processes possessing different dual combinations and following this, to obtain reuse water during the process at relatively high rates in comparison to the feed volume for industrial operations via other complementary membrane process applications that are carried out in the second step.
  • membrane process content such as whey concentration, water recovery for reuse and obtaining whey powder
  • Another aim of the invention is to carry out a method where concentrated why stream production is provided having higher solid content (%25-35) and where industrial reuse water is produced at high volumes (%65-80) by increasing the whey that is a by product of the cheese production industry, focusing on achieving treatable concentrated whey production having lower drying costs during whey powder production, together with lower whey concentration costs using novel integrated industrial membrane systems.
  • Proposed innovative membrane systems is designed for three different combinations consisting of FO/RO, FO/MD and MD/RO with regard to membrane process content.
  • the systems are technologically classified into two different bases which are related to the characteristic of innovative membrane process which is applied in the first step.
  • first membrane operating step of the system which is aimed to achieve concentration of raw whey, dehydration and producing a concentrate whey stream
  • two distinctive technological configurations are constituted for situations of utilization of FO and MD processes
  • membrane systems designed for "First step with FO and with MD” different membrane application technologies are illustrated in Figure 1 and Figure 2, respectively, in order of process flow diagram including whey powder production from concentrated whey.
  • Figure 1 - Is the schematic representation of FO/RO or FO/MD innovative combined membrane systems including whey concentration, water recovery and whey powder production by industrial whey treatment and
  • Figure 2 - Is the schematic representation of MD/RO innovative combined membrane system including whey concentration, water recovery and whey powder production by industrial whey treatment.
  • stage (optional) RO process feed line for FO/RO II.
  • stage (optional) RO process for FO/RO
  • stage (optional) RO process for FO/RO Membrane concentrate line of II.
  • stage (optional) RO process for FO/RO Membrane concentrates collection and distribution structure of I. and II. stages (optional) RO processes for FO/RO,
  • FO/RO and FO/MD integrated membrane system configurations are applied.
  • the raw whey which first of all is received from cheese production process is delivered to the raw whey storage tank (2) via the filling line (1).
  • the raw whey is fed to the FO module feed flow channel of the FO process module (4) via the FO process feed line (3).
  • the FO draw solution is fed from the FO draw solution storage tank (6) via the feed line (7), and as a result the passage of an amount of water in raw whey into the draw solution is provided.
  • the concentrated whey using the FO process in FO/RO and FO/MD systems and the MD process of the MD/RO system, that is delivered through the concentrate whey effluent line (5), is submitted to the concentrate whey storage tank (25) in order to produce whey powder.
  • FO draw solution which is diluted by water withdrawn from whey, is recycled to the FO draw solution storage tank (6) through the diluted FO draw solution return line (12) by sending it to the diluted FO draw solution stream distribution line (9) through the diluted FO draw solution return line (8); thus, closed loop operation of FO draw solution line can be enabled.
  • Membrane process at the second step for the FO/RO system is optionally applied in sequential two stages; while application of MD process in FO/MD system is carried out in a single stage.
  • stage RO application becomes mandatory to obtain clean water.
  • the membrane concentrate is delivered to the membrane concentrates collection and distribution structure (23) (optional RO application is not provided for FO/MD) of the I. II stage (optional) RO process for FO/RO via the I. stage RO for FO/RO and the MD process membrane concentrate line (15) for FO/MD, the filtered water is then delivered to the filtered water stream collection and distribution structure (17) processed with MD for FO/MD or I.
  • Stage RO for FO/RO via the filtered water effluent line (16) processed with MD for FO/MD or I.
  • stage RO for FO/RO and is obtained as process water over the reuse water effluent line (18) during the production process of MD for FO/MD or I.
  • Stage RO for FO/RO if optional II stage RO application is not necessary.
  • a portion of or all of the filtered effluent water of I. stage RO or MD process (14) for FO/MD is fed to II. stage (optional) RO process (20) for FO/RO with the connection of II. stage (optional) RO process feed line (19) for FO/RO, via the I. stage RO for FO/RO or MD process for FO/MD filtered water stream collection and distribution structure (17).
  • process water is obtained through the II. stage (optional) RO process for FO/RO recovery water effluent line (21).
  • Membrane concentrate stream belonging to II. stage RO process is first submitted to I. and II. stage (optional) RO process membrane concentrates collection and distribution structure (23) for FO/RO via the II.
  • stage RO membrane concentrate belonging to I. stage RO for FO/RO or MD process for FO/MD is recycled back to the FO draw solution storage tank (6) under a closed loop via the I. stage for FO/RO and MD process membrane concentrate transfer line (15) for RO or FO/MD, and to the I. and II. stage (optional) RO flow collection and distribution structure (23) for FO/RO and to the FO draw solution return line (24) of the MD process membrane concentration for FO/MD or RO processes for FO/RO.
  • Stage RO application the II stage RO membrane concentrate, is included into a loop via the II.
  • the raw whey which first of all is received from cheese production process is delivered to the raw whey storage tank (2) via the filling line (1).
  • MD process (32) which is the first step membrane process of the system via the feed line (31).
  • Filtered water in the MD process is sent to the RO process (34) which is the second step membrane process via the MD process filtered water effluent line (33).
  • Whey which is concentrated during the MD process is delivered to the concentrated whey storage tank (25) for the purpose of whey powder production via the concentrated whey effluent line (5) from the FO process in FO/RO and FO/MD systems and from the MD process in MD/RO systems.
  • Re-filtration of the MD filter effluent water during the RO process the water production of recovered water quality for the production process is provided via the RO process filter water effluent line (35). Additionally, cyclical operation of the MD/RO system under closed loop is carried out by sending the RO process concentrate stream to the whey collection and distribution structure (30) via the return line (36).
  • whey powder production from whey streams (5) concentrated at the first step membrane processes is carried out in common production processes such as the FO process in FO/RO and FO/MF systems and the MD process in MD/RO systems.
  • both two innovative membrane systems classified technologically, upon the first step membrane process become integrated by combining them with whey powder production.
  • a concentrated whey stream in relative high solid content is obtained by recovery of process water in high volume in the systems; on the other hand because of increased solid content of concentrated whey, production of whey powder is carried out economically by removing water of concentrated whey under relatively lower energy consumption.
  • whey concentrated by both technological configurations such as from the FO process in FO/RO and FO/MF systems and from the MD process in the MD/RO processes is submitted to the storage tank (25) via effluent line (5), and is then transferred to unit where water removal processes such as concentrated whey evaporation or drying (27) are carried out with the transfer line (26).
  • Whey dewatered in this unit is produced as powder via whey powder the effluent line (29).
  • organic vapour emissions originating from volatile organics in whey are present besides presence of water vapour.
  • organic pollutants which are in the vapour phase are taken to liquid phase.
  • membrane modules can be carried out by utilizing different structured membrane modules (tubular, hollow fibre, spiral wound or flat sheet) independent of their geometry. Every individual membrane system, by also taking into account process specific technical necessities; is provided as comprising technical equipment such as pumps, pressure gauges, flow control valves, temperature control (heating/cooling) units, gas control and release valves.
  • Operating of membrane systems can be designed to be intermittent, semi-continuous or continuous depending on the purpose of use, quality content of whey and influent flow rate of system.

Landscapes

  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Dairy Products (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention concerne un procédé basé sur l'utilisation de systèmes de membrane innovants avec différentes combinaisons, qui concerne le lactosérum en tant qu'eau usée de production de fromage qui devrait être significativement pris en compte en termes de pollution environnementale par l'industrie laitière; par rapport à des combinaisons de processus à membrane entraînés par pression couramment utilisés (32 à 40 % de récupération d'eau et production de lactosérum concentré à une teneur en matières solides de 15 à 20 %), dont l'objectif principal est de récupérer de l'eau à partir de lactosérum à des pourcentages de récupération d'eau plus élevés (65 à 80 %) ayant une qualité réutilisable dans le processus de production est de permettre techniquement et commercialement une production économique augmentée de poudre de lactosérum au moyen de l'obtention de lactosérum concentré ayant des pourcentages en matières solides plus élevés (25 à 35 %).
PCT/TR2016/050573 2016-02-15 2016-12-29 Procédé de récupération à volume élevé d'eau de traitement et d'acquisition de produit économique à partir de lactosérum Ceased WO2017142494A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
TR2016/01884 2016-02-15
TR201601884 2016-02-15

Publications (1)

Publication Number Publication Date
WO2017142494A1 true WO2017142494A1 (fr) 2017-08-24

Family

ID=58213313

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/TR2016/050573 Ceased WO2017142494A1 (fr) 2016-02-15 2016-12-29 Procédé de récupération à volume élevé d'eau de traitement et d'acquisition de produit économique à partir de lactosérum

Country Status (1)

Country Link
WO (1) WO2017142494A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2019063773A (ja) * 2017-10-04 2019-04-25 水ｉｎｇ株式会社 廃水の濃縮方法及び廃水の濃縮装置
JPWO2021054406A1 (fr) * 2019-09-17 2021-03-25
EP3892098A1 (fr) * 2020-04-11 2021-10-13 DMK Deutsches Milchkontor GmbH Procédé pour la préparation de poudres de produits thermolabiles
CN115530237A (zh) * 2021-06-30 2022-12-30 内蒙古伊利实业集团股份有限公司 一种基于正渗透的浓缩乳制备方法及其应用
US12404196B2 (en) 2020-11-10 2025-09-02 Complete Filtration Resources, Inc. Systems and methods for removing phosphorus from water

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA966361A (en) 1970-07-24 1975-04-22 Charles E. Zanzig Whey treatment process and product
US3880755A (en) * 1973-05-22 1975-04-29 Osmonics Inc Method and apparatus for separating cheese whey protein
US4617861A (en) * 1982-10-07 1986-10-21 Fermentation Engineering, Inc. Whey treatment apparatus
CA2244109A1 (fr) * 1996-02-05 1997-08-14 Veikko Jolkin Procede de traitement de petit lait
US5679780A (en) 1992-05-07 1997-10-21 Tetra Laval Holdings & Finance S.A. Method for obtaining high-quality protein products from whey
EP1046344A2 (fr) 1999-04-22 2000-10-25 Snow Brand Milk Products, Co., Ltd. Concentré de protéines de lactosérum et procédé de préparation
CA2778360A1 (fr) * 2009-10-28 2011-05-05 Valio Ltd. Produit a base de proteines lactoseriques et son procede de preparation
WO2012116409A1 (fr) * 2011-03-03 2012-09-07 Victoria University Système d'échange de chaleur
US20130220927A1 (en) * 2011-04-08 2013-08-29 Charles D. Moody Forward Osmosis: Recyclable Driving Solutes

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA966361A (en) 1970-07-24 1975-04-22 Charles E. Zanzig Whey treatment process and product
US3880755A (en) * 1973-05-22 1975-04-29 Osmonics Inc Method and apparatus for separating cheese whey protein
US4617861A (en) * 1982-10-07 1986-10-21 Fermentation Engineering, Inc. Whey treatment apparatus
US5679780A (en) 1992-05-07 1997-10-21 Tetra Laval Holdings & Finance S.A. Method for obtaining high-quality protein products from whey
CA2244109A1 (fr) * 1996-02-05 1997-08-14 Veikko Jolkin Procede de traitement de petit lait
EP1046344A2 (fr) 1999-04-22 2000-10-25 Snow Brand Milk Products, Co., Ltd. Concentré de protéines de lactosérum et procédé de préparation
CA2778360A1 (fr) * 2009-10-28 2011-05-05 Valio Ltd. Produit a base de proteines lactoseriques et son procede de preparation
WO2012116409A1 (fr) * 2011-03-03 2012-09-07 Victoria University Système d'échange de chaleur
US20130220927A1 (en) * 2011-04-08 2013-08-29 Charles D. Moody Forward Osmosis: Recyclable Driving Solutes

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
COSKUN AYDINER ET AL: "Techno-economic viability of innovative membrane systems in water and mass recovery from dairy wastewater", JOURNAL OF MEMBRANE SCIENCE, vol. 458, 1 May 2014 (2014-05-01), NL, pages 66 - 75, XP055363329, ISSN: 0376-7388, DOI: 10.1016/j.memsci.2014.01.058 *

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2019063773A (ja) * 2017-10-04 2019-04-25 水ｉｎｇ株式会社 廃水の濃縮方法及び廃水の濃縮装置
JP7085329B2 (ja) 2017-10-04 2022-06-16 水ｉｎｇ株式会社 廃水の濃縮方法及び廃水の濃縮装置
JPWO2021054406A1 (fr) * 2019-09-17 2021-03-25
JP7249427B2 (ja) 2019-09-17 2023-03-30 旭化成株式会社 原料液濃縮方法および原料液濃縮システム
US12576362B2 (en) 2019-09-17 2026-03-17 Asahi Kasei Kabushiki Kaisha Method for concentrating raw material solution, and system for concentrating raw material solution
EP3892098A1 (fr) * 2020-04-11 2021-10-13 DMK Deutsches Milchkontor GmbH Procédé pour la préparation de poudres de produits thermolabiles
US12404196B2 (en) 2020-11-10 2025-09-02 Complete Filtration Resources, Inc. Systems and methods for removing phosphorus from water
CN115530237A (zh) * 2021-06-30 2022-12-30 内蒙古伊利实业集团股份有限公司 一种基于正渗透的浓缩乳制备方法及其应用

Similar Documents

Publication Publication Date Title
US9427705B1 (en) Method of solvent recovery from a dilute solution
US9102544B2 (en) Wastewater treatment system
Macedonio et al. Pressure-driven membrane operations and membrane distillation technology integration for water purification
US7459088B2 (en) Water desalination process and apparatus
US8147697B2 (en) Apparatus and process for desalination of brackish water
US9822021B2 (en) Forward osmosis separation processes
Wenten et al. Integrated processes for desalination and salt production: A mini-review
WO2017142494A1 (fr) Procédé de récupération à volume élevé d'eau de traitement et d'acquisition de produit économique à partir de lactosérum
WO2020049579A1 (fr) Systèmes combinatoire à base de membranes et procédés de déshydratation et de concentration d'applications
US20120231535A1 (en) Organic Forward Osmosis System
US20140157846A1 (en) Methods and systems for treating bioreactor wastewater streams
CN205340584U (zh) 用于提高盐水浓度的渗透驱动膜系统和处理
Chen et al. Separation technologies for salty wastewater reduction in the dairy industry
US20260008014A1 (en) Method and system for extraction of minerals based on divalent cations from brine
CA2672790C (fr) Procede de traitement d'un flux de substance
Chowdhury et al. Membrane-based technologies for industrial wastewater treatment and resource recovery
WO2017078644A2 (fr) Procédé de récupération de solvant à partir d'une solution diluée
Benbouzid et al. Analysis and simulation of a reverse osmosis unit for producing drinking water in Morocco
CN110526474A (zh) 一种反渗透浓水的提浓减量方法及提浓减量装置
CN105836976A (zh) 长链二元烷酸结晶母液的综合处理方法
Nath et al. Fundamentals of membranes for wastewater treatment: Challenges and opportunities for resource recovery
Agrawal et al. Forward Osmosis: An Energy-Efficient Approach for the Treatment and Recovery of Resources from the Dairy Industry Effluent: Forward Osmosis Treatment of Dairy Industry Waste Stream Whey
Dhume et al. Membrane Technology for Green Engineering
US20230357096A1 (en) Method for manufacturing organic liquid fertilizer
WO2025046454A1 (fr) Système intégré et procédé de récupération d'eau potable et de sels à partir d'eau de mer menant à des zld

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 16843213

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 16843213

Country of ref document: EP

Kind code of ref document: A1